Process for producing diphenylamines or N,N&#39;-diphenyl-phenylenediamines

ABSTRACT

Diphenylamines or N,N&#39;-diphenyl-phenylenediamines can be obtained by heat-reacting an aniline or a phenylenediamine with preferably an excess of a phenol in an amount of 4 to 20 moles per mole of the aniline or phenylenediamine in th presence of a hydrogen transfer catalyst and a cyclohexanone corresponding to said phenol. 
     The excess phenol used in the reaction undergoes reduction in the reaction system to form a cyclohexanone, which in turn reacts with the aniline or phenylenediamine to form a Schiff base and is thus consumed. The Schiff base forms the intended product by means of a dehydrogenation reaction, and the hydrogen evolved at this time reduces the phenol to form a cyclohexanone. 
     The phenol present in excess thus becomes in the system a solvent, a starting material for the cyclohexanone, and an acceptor of the hydrogen that forms as a by-product at the time of formation of the intended product. Hence, it becomes possible to obtain the intended product at a high selectivity from the anilines and phenylenediamines. 
     The process of this invention is an advantageous process for the industrial production of especially the nuclearly substituted diphenylamines.

This is a continuation of application Ser. No. 080,440, filed on July31, 1987, now U.S. Pat. No. 4,804,780 (a) which is a continuation ofapplication Ser. No. 903,427, filed on Sept. 4, 1986, now abandoned,which is a divisional of application Ser. No. 710,662, filed on Mar. 12,1985, now abandoned, and (b) which is a continuation of application Ser.No. 710,662, filed on Mar. 12, 1985, now abandoned.

This invention relates to a process for producing the diphenylamines orN,N'-diphenyl-phenylenediamines. More specifically, this inventionrelates to a process for producing the diphenylamines orN,N'-diphenyl-phenylenediamines by heat-reacting an aniline or aphenylenediamine with a phenol in the presence of a hydrogen transfercatalyst and a cyclohexanone corresponding to said phenol, using thephenol in an excessive amount to the aniline or phenylenediamine.

The anilines, as used herein, are compounds of the formula ##STR1##wherein R is hydrogen or a lower alkyl group, and X and Y are hydrogen,fluorine, or an alkyl, alkoxy, carboxyl, carboxyl esters, cyano,hydroxyl or benzyl group, which substituents may be the same ordifferent. And the phenylenediamines, as used herein, are compounds ofthe formula ##STR2## wherein X is hydrogen or a lower alkyl group. Onthe other hand, the phenols corresponding to the cyclohexanones arecompounds of the formula ##STR3## wherein X is a lower alkyl group or alower alkoxy group, and n is an integer from 0 to 2.

The process of this invention is an especially advantageous method forproducing industrially the nuclearly substituted diphenylamines from thenuclearly substituted products of aniline of the formula (1) that havebeen substituted by the alkyl groups and/or alkoxy groups and/orfluorine.

The diphenylamines and N,N'-diphenyl-phenylenediamines are compoundsthat are useful as intermediates for the production of dyestuffs,agricultural chemicals, medicines, rubber compounding agents, etc. Thenuclearly substituted diphenylamines, for example,2-methyl-4-alkoxydiphenylamine and2-methyl-4-alkoxy-2',4'-dimethyl-diphenylamine, as starting materialsfor dyes for use with the fluoran-type pressure-sensitive orheat-sensitive recording papers, and 2-chloro-5-methyl-diphenylamine, asa starting material of agricultural chemicals, are especially expensiveand valuable compounds.

In the past, the known processes for producing the diphenylaminesinclude that in which the diphenylamines are produced by a deammoniationreaction from such amines as aniline or that in which the diphenylaminesare produced by either a dehydration or dehydrobromination reaction fromamines and phenols or bromobenzene. As specific suggestions, there hasbeen proposed a process for producing a diphenylamine from a phenol andaniline using gamma-alumina as catalyst (Japanese Patent Publication No.14738/1974), and a process involving acetylation of2-methyl-4-methoxyaniline, reacting the resulting product withbromobenzene, and thereafter hydrolyzing the resulting2-methyl-4-methoxy-N-acetyldiphenylamine to give2-methyl-4-methoxydiphenylamine (Japanese Patent Publication No.5489/1977).

On the other hand, as processes for producing the N-alkyldiphenylamines,known are such processes as that wherein a diphenylamine is reacted withan alkyl halogenide, dialkyl sulfate or trialkyl phosphate, and that inwhich a hydrochloride of diphenylamine and alcohol are reacted. And asthe process for producing the N,N'-diphenyl-phenylenediamines, known isthat in which phenylenediamine, dihydroxybenzene or disulfoxybenzene,and aniline or a salt thereof are reacted.

All of the foregoing processes are however extremely unsatisfactory foruse as industrial processes.

As a process differing from the foregoing processes, also known is aprocess which involves reacting an amine with a Schiff base.Specifically, there has been suggested a process involving reactionN-cyclohexylideneaniline in the vapor phase with an oxygen-containinggas in the presence of an oxidizing catalyst such as silica (JapaneseLaid-Open Patent Publication No. 49,924/1974), or a process whichcomprises heat-reacting N-methylaniline and cyclohexanone in thepresence of a palladium catalyst and thereafter submitting the resultingSchiff base to a dehydrogenation reaction to give N-methyldiphenylamine(U.S. Pat. No. 3,219,704). The dehydrogenation reaction of theseprocesses are however carried out in the absence of a hydrogen acceptor,with the consequence that the yields are unsatisfactory low valuesdespite the fact that the N-methylaniline and cyclohexanone are used ina nearly equivalent ratio.

Further, there has also been suggested a process which uses a styrene asthe hydrogen acceptor in producing diphenylamines via a Schiff base suchas N-cyclohexylideneaniline by reacting an amine with a cyclohexanone inthe presence of a hydrogenating catalyst such as a palladium catalyst(Japanese Laid-Open Patent Publication No. 58,648/1982).

Specifically, this process is a process for obtaining4-aminodiphenylamine from p-phenylenediamine. This process is on thewhole satisfactory as regards its reaction rate and selectivity.However, for obtaining the intended product this process requires theuse of an aniline and a substantially equivalent amount of acyclohexanone. And the not readily available cyclohexanones must besynthesized from the phenols in a separate step. Further, the styrenesare only utilized as a hydrogen acceptor. This process thus cannot beregarded as being an industrially satisfactory process for producing thediphenylamines.

If a more detailed description is made, in the process of the foregoingJapanese Laid-Open Patent Publication No. 58,648/1982 the styrene addedas a hydrogen acceptor becomes catalytically hydrogenated to become anentirely different compound that cannot be incorporated into thereaction system of this process, and it thus cannot be recycled forreuse. Hence, unless there can be conceived an effective use for thiscompound, the process becomes extremely costly when appliedindustrially. Further, since the styrene, as described above, becomescatalytically hydrogenated to become an entirely different compound thatcannot be incorporated into the reaction system of this process, theproportion in which the amines and cyclohexanones used must be broughtas close as possible to the equivalent ratio. Otherwise, a separate stepfor separating and purifying the excess amines and/or cyclohexanoneswill be required, or a loss in the amines or cyclohexanones will bebrought about.

An object of the present invention is therefore to improve on thesedefects of the conventional processes.

The present inventors have engaged in extensive investigations with theview of achieving this object. These investigations led to the discoverythat when an aniline of the aforesaid formula (1) or a phenyldiamine ofthe formula (2) (for brevity, these are referred to hereinafter asamines) is heat-reacted in the presence of a hydrogen transfer catalystand an excess of a phenol, with a cyclohexanone corresponding to thephenol, the formation of a Schiff base as a result of a condensationreaction between the amine and the cyclohexanone takes place, as well asits dehydrogenation reaction is set up, and simultaneously there isformed afresh in the same reaction system by the reduction of phenol acyclohexanone in an amount corresponding to that consumed in thecondensation reaction. It was hence found that the reaction proceedsreadily simply by causing the presence of a catalytic amount of thecyclohexanone in the early stage of the reaction, and moreover that eventhough the amine has a nuclearly substituted group the intended productcan be obtained at a high selectivity by carrying out the reaction inthe presence of an excess of the phenol.

There is thus provided in accordance with this invention a process forproducing diphenylamines either by heat-reacting an amine and an excessof a phenol in the presence of a hydrogen transfer catalyst and acatalytic amount of a cyclohexanone corresponding to the phenol of theaforesaid formula (3) used in the reaction; or by a procedure in whichthe cyclohexanone is not caused to be present in the reaction systemfrom the outset but by heat-reacting a phenol with an amine whileconverting a part of the excessively charged phenol under hydrogenpressue to its corresponding cyclohexanone.

The process of this invention not only gives satisfactory results inrespect of the reaction rate and the selectivity for the intendedproduct, but also since the phenols are hydrogen acceptors as well asthe supply source of the cyclohexanones that are formed as a result oftheir being hydrogen acceptors, there is the advantage that thecyclohexanone-containing phenols that are separated at the time ofrecovery of the intended diphenylamines can be directly recycled andreused in the reaction system in their as-mixed state. Further, in theprocess of this invention hydrogen is formed by dehydrogenation of theSchiff base, the intermediate product, formed by the reaction betweenthe amines and the cyclohexanones, and the so formed hydrogen isutilized in the same reaction system in reducing the phenols, i.e., theformation of the cyclohexanones. The process is thus extremelyefficient. Again, in the case of some types of the nuclearly substituteddiphenylamines difficulty is experienced in producing these by asingle-stage reaction, but in accordance with the process of thisinvention the synthesis of these compounds by a single-stage reaction ispossible. And even in those cases where the suitable correspondingcyclohexanones are not easily available, there is the advantage that inaccordance with the process of this invention the reaction can becarried out by using in place of such cyclohexanones an excess of thephenols and carrying out the reaction while converting a part of thephenols to cyclohexanones under hydrogen pressure.

As the phenols to be used as the starting material in the process ofthis invention, included are, for example, phenol; the alkyl phenolssuch as methylphenol, ethylphenol, isopropylphenol, butylphenol,2,4-dimethylphenol, 2,4,6-trimethylphenol and2,6-di-t-butyl-4-methylphenol; and the alkoxy phenols such as3-methoxyphenol and 4-methoxyphenol, especially preferred being phenol.

As to the amount of the phenols to be used, while the reaction proceedswith an amount equivalent to the amines when the cyclohexanones are usedfrom the outset, there is a tendency to a decline in the selectivity.Hence, the phenols must be used in excess, i.e., at least 2 moles, andpreferably from 4 to 20 moles, per mole of the amines.

As the aniline of the aforesaid formula (1), there can be named, forexample, aniline, N-alkylanilines and the nuclearly substituted productsof these anilines. All of these can give the corresponding intendedproduct at high selectivities. From the standpoint of the demand for theproduct, it is however advantageous commercially to apply the process ofthis invention to the nuclearly substituted products. Examples of thenuclearly substituted products include such alkyl anilines as2-methylaniline; such dialkyl anilines as 3,4-dimethylaniline; suchalkoxy anilines as 3-methoxyaniline; such alkylalkoxy anilines as2-methyl-4-methoxyaniline; o-aminobenzoic acid and esters thereof;o-aminobenzonitrile; 4-benzylaniline; aminophenol; and the fluoro alkylanilines such as 2-fluoro-5-methylaniline. And as the N-alkyl group ofthe N-alkylanilines, included are say methyl, ethyl and propyl.

On the other hand, as the phenylenediamines of the aforesaid formula(2), there can be named, for example, p-phenylenediamine, m-phenylenediamine, o-phenylenediamine and toluenediamine.

Usable as the cyclohexanones are those corresponding to the phenolsmentioned hereinbefore. The use of the cyclohexanones in a catalyticamount will do, and usually, if it is used in an amount of at leastabout 0.03 mole per mole of the amines, no special problems will arise.When the amine is an aniline of formula (1), it is preferably used in anamount of 0.05 to 0.40 mole per mole of the amine. On the other hand,when the amine is a phenylenediamine of formula (2), it is preferablyused in an amount of at least 0.5 mole per mole of the amine. When theamount used is less than these amounts, the reaction rate is reduced,whereas when the amount exceeds these amounts, this also is undesirable,since a decline takes place in the yields of the intended diphenylaminesand N,N'-diphenylene-diamines.

On the other hand, when the cyclohexanones are not used from the outsetof the reaction, the following procedure will do. To wit, theheat-reaction is carried out after introducing and sealing in thereactor hydrogen in an amount corresponding to that which forms thecyclohexanone in a proper amount such as indicated hereinabove, i.e., onthe basis of the phenols, at least about 0.06 mole (preferably from 0.10to 0.80 mole when the amine is an aniline and at least 0.6 mole when theamine is a phenylenediamine).

The catalyst used in the process of this invention must be one havingthe function of catalyzing both the dehydrogenation and reductionreactions. Usually, a suitable hydrogenating catalyst is also suitablyused with the dehydrogenation reaction. Specific examples of such acatalyst are the supported Raney nickel, reduced nickel or nickelcatalysts, supported Raney cobalt, reduced cobalt or cobalt catalysts,supported Raney copper, reduced copper or copper catalysts, catalysts ofthe noble metals of group VIII of the periodic table or catalystsobtained by supporting these metals on a carrier material such ascarbon, alumina or barium carbonate, rhenium catalysts such asrhenium-carbon, and the copper-chromate catalysts. Of these catalysts,preferred is palladium, and especially preferred are such supportedcatalysts of palladium as palladium-carbon, palladium-alumina andpalladium-magnesium oxide. These catalysts are used, based on theamines, in an amount calculated as metal atoms, of usually 0.001 to 0.2gram-atom, preferably 0.004 to 0.1 gram-atom.

A reaction temperature of 130° to 350° C. is usually employed. When theamine is aniline or its nuclearly substituted product, a temperature inthe range of 170° to 280° C. is preferably chosen, whereas when theamine is an N-alkylaniline or its nuclearly substituted product, atemperature in the range of 130° to 200° C. is preferably chosen.

The intended diphenylamines can be obtained by treating thereaction-completed mixture in customary manner, for example,distillation, crystallization or extraction. At this time, as apreferred mode of practicing the invention process, thecyclohexanone-containing excess phenol obtained after completion of thereaction is recycled in its as-obtained state for reuse in the secondand subsequent reactions. Specifically, the liquid obtained aftercompletion of the reaction is filtered to separate the catalyst, whichcan be reused. The filtrate is then concentrated, and thecyclohexanone-containing phenol is recovered, followed by returning thisfraction to the reaction system in its as-mixed state. The diphenylamineremaining in the kettle is then purified and separated by saydistillation, crystallization, etc.

The industrially valuable and expensive diphenylamines orN,N'-diphenyl-phenylenediamines can thus be easily obtained from theamines in accordance with the process of this invention. For example,2-methyl-4-methoxy-diphenylamine could only be obtained by roundaboutmethods such as the process disclosed in Japanese Patent Publication No.5489/1977, which is carried out in accordance with the followingreaction scheme: ##STR4## or the process disclosed in Japanese Laid-OpenPublication No. 136,252/1980, which is carried out in accordance withthe following reaction scheme: ##STR5## It is now however possible bythe utilization of the process of this invention to obtain2-methyl-4-methoxydiphenylamine from 2-methyl-4-methoxyaniline andphenol in a single stage and moreover in a high yield. The process ofthis invention can therefore be regarded as being an extremelyadvantageous process for say the industrial production of2-alkyl-4-alkoxydiphenylamines.

The following examples will serve to illustrate the process of thepresent invention more specifically.

EXAMPLE 1

A 500-ml stainless steel autoclave was charged with 21.4 g (0.2 mole) of2-methylaniline, 94.1 g (1.0 mole) of phenol, 2.0 g (0.02 mole) ofcyclohexanone and 1.07 g of 5% palladium-carbon (product of JAPANENGELHARD LTD.). After purging the inside of the autoclave withnitrogen, the temperature was raised to 200° C., after which thereaction was carried out at this temperature for 3 hours with stirring.The temperature was then returned to room temperature, after which thereaction mixture was filtered to separate a catalyst.

A part of the filtrate was taken, and the unreacted starting materialsand product were quantitatively determined by gas chromatography. Theanalysis showed that 0.3 g (conversion 98.6%) of unreacted2-methylaniline remained and that 35.8 g (selectivity 99.2%) had beenformed. The filtrate was then distilled to concentrate and separate, andrecover 6.0 g of a fraction of phenol containing cyclohexanone. Theconcentration of cyclohexanone in the fraction was 2.4%, whichcorresponds to 91.2% of the amount of cyclohexanone charged. Theconcentrated liquid obtained after separation of the phenol was againdistilled under reduced pressure to give 34.8 g (yield 95%) of afraction boiling at 173° to 179° C. at a reduced pressure of 20 mmHg.

This was followed by carrying out the reaction in like manner but addingonly 20.0 g of phenol to the aforesaid recovered catalyst and recoveredphenol fraction containing cyclohexanone and without the addition afreshof cyclohexanone. This reaction gave 2-methyl-diphenylamine at aconversion of 97.7% and a selectivity of 99.3%. The cyclohexanoneconcentration in the phenol fraction was 2.2%.

EXAMPLE 2

A 500-ml stainless steel autoclave was charged with 64.2 g (0.6 mole) of2-methylaniline, 56.5 g (0.6 mole) of phenol, 6.0 g (0.06 mole) ofcyclohexanone and 3.2 g of 5% palladium-carbon. After the inside of theautoclave was purged with nitrogen, the temperature was raised to 200°C., and the reaction was carried out for 7 hours at this temperaturewith stirring. After completion of the reaction, the reaction productwas treated as in Example 1 and then analyzed in the same manner. It wasfound as a result of the analysis that 1.2 g (conversion 98.1%) ofunreacted 2-methylaniline remained and that 98.5 g (selectivity 91.3%)of 2-methyl-diphenylamine had been formed. These results show that theuse of phenol in the reaction in an equivalent amount was adisadvantage.

EXAMPLE 3

The reaction was carried out in the same manner as in Example 1 butusing 5% palladium-magnesium oxide instead of 5% palladium-carbon, afterwhich the reaction product was treated in like manner.

As a result of the foregoing experiment, 1.2 g (conversion 94.4%) ofunreacted 2-methylaniline remained and 33.1 g (selectivity 95.8%) of2-methyl-diphenylamine was formed.

EXAMPLE 4

A 500-ml autoclave of the same type as used in Example 1 was employed,and this autoclave was charged with the same charge materials as inExample 1, except that the initially charged cyclohexanone was absent.After purging the inside of the autoclave with nitrogen, a pressure of 5kg/cm².G was built up with hydrogen. The amount of this hydrogencorresponds to about 0.3 mole per mole of the 2-methylaniline (i.e. 0.3mole as the amount of cyclohexanone formed from the phenol used in thereaction). The reaction was carried out in the same manner as in Example1 followed by the same treatment.

As a result of having carried out the experiment in this manner, therewas formed 2-methyl-diphenylamine at a selectivity of 99.0%. Andcyclohexane was present in the recovered phenol fraction, and itsconcentration was 3.3%.

EXAMPLE 5

Example 1 was repeated but using 3,4-dimethoxyaniline instead of2-methylaniline. Unreacted 3,4-dimethoxyaniline was not noted, and3,4-dimethoxydiphenylamine was obtained at a selectivity of 97.0%.

EXAMPLE 6

The experiment was carried out as in Example 1 but using2-methyl-4-methoxyaniline instead of 2-methylaniline. At a conversion of98.0%, 2-methyl-4-methoxy-diphenylamine was formed at a selectivity of98.0%.

The filtrate resulting after separation of the catalysts wasconcentrated to separate and recover a phenol fraction, after which theconcentrated liquid was distilled under reduced pressure to give 39.3 g(yield 94.0%) of a fraction boiling a 192° to 198° C.

EXAMPLE 7

Example 1 was repeated but using 2,4-dimethylphenol instead of phenol.At a conversion of 98.5%,2-methyl-4-methoxy-2',4'-dimethyl-diphenylamine was formed at aselectivity of 93.0%.

EXAMPLE 8

The experiment was conducted as in Example 1 but using2-fluoro-5-methylaniline instead of 2-methylaniline, whereupon a virtualcompletion of the reaction was achieved, and2-fluoro-5-methyl-diphenylamine was obtained at a selectivity of 95.5%.

EXAMPLE 9

A 500-ml stainless steel autoclave was charged with 24.2 g (0.2 mole) of2-methyl-N-methylaniline, 94.1 g (1.0 mole) of phenol, 2.0 g (0.02 mole)of cyclohexanone and 1.07 g of 5% palladium-carbon. After purging theinside of the autoclave with nitrogen, the temperature was raised to150° C. The reaction was then carried out for 8 hours at thistemperature with stirring, after which the temperature was cooled toroom temperature, and the reaction mixture was filtered to separate acatalyst.

A part of the filtrate was taken, and the unreacted starting materialsand the product were quantitatively determined by gas chromatography.The analysis showed that 0.8 g (conversion 96.7%) of2-methyl-N-methylaniline remained and 33.8 g (selectivity 88.7%) of2-methyl-N-methyl-diphenylaniline had been formed. The filtrate wasdistilled to concentrate and separate, and recover 75.8 g of a fractionof phenol containing cyclohexanone. The concentration of cyclohexanonein the fraction was 2.2%, and this corresponds to 83.4% of the amount ofcyclohexanone charged.

This was followed by carrying out the reaction in like manner but addingonly 20.0 g of phenol to the aforesaid recovered catalyst and recoveredphenol fraction containing cyclohexanone and without the addition afreshof cyclohexanone. This reaction gave 2-methyl-N-methyl-diphenylamine ata conversion of 96.0% and a selectivity of 90.0%. The cyclohexanoneconcentration in the recovered phenol fraction was 2.4%.

EXAMPLE 10

Example 9 was repeated but using 2-methyl-4-methoxy-N-methylanilineinstead of 2-methyl-N-methylaniline. The intended product was obtainedin this case at a conversion of 97.5% and a selectivity of 89.0%.

EXAMPLE 11

A 500-ml stainless steel autoclave was charged with 21.6 g (0.2 mole) ofm-phenylenediamine, 141.2 g (1.5 mole) of phenol, 9.8 g (0.1 mole) ofcyclohexanone and 2.16 g of 5% palladium-carbon. After purging theinside of the autoclave with nitrogen, the temperature was raised to200° C. After carrying out the reaction at this temperature for 12 hourswith stirring, the autoclave was cooled to room temperature, and thereaction mixture was filtered to separate a catalyst.

A part of the filtrate was taken and analyzed by gas chromatography. Itwas found that 52.1 g (yield 91.0%) of N,N'-diphenyl-m-phenylenediaminehad been formed. The filtrate was distilled to concentrate and separate,and recover 96.8 g of a phenol fraction containing cyclohexanone. Theconcentration of cyclohexanone therein was 8.7%, which corresponds to85.9% of the amount of cyclohexanone charged.

This was followed by carrying out the reaction in like manner, adding52.8 g of phenol and 0.032 g of a fresh catalyst to the aforesaidrecovered catalyst and recovered cyclohexanone-containing phenolfraction but without the addition afresh of cyclohexanone.N,N'-diphenyl-m-phenylenediamine was thus obtained at a yield of 90.3%.And the concentration of cyclohexanone in the recovered phenol fractionwas 9.0%.

EXAMPLE 12

Example 9 was repeated but using 3,5-dimethylphenol instead of phenol.There was thus obtained N,N'-di(3,5-dimethylphenol)-m-phenylenediamineat a yield of 89.2%. 3,5-Dimethylcyclohexanone was present in therecovered 3,5-xylenol fraction at a concentration of 8.6%.

What is claimed is:
 1. A process for producing aN,N'-diphenylphenylenediamine, which comprises heat-reactingp-phenylenediamine with an excess of phenol or 3,5-dimethylphenol, saidreaction being carried out in the presence of a hydrogen transfercatalyst and at least 0.5 mole per mole of the p-phenylenediamine ofcyclohexanone corresponding to said phenol or 3,5-dimethyl-phenol, andsaid phenol being used in an excess of 4 to 20 moles per mole of saidp-phenylenediamine.
 2. The process as claimed in claim 1 which comprisesseparating the N,N'-diphenylphenylenediamine from the heat-reductionmass, and thereafter recycling the cyclohexanone-containing phenol tothe reaction system for reuse.
 3. Process for producing aN,N'-diphenylphenylenediamine, which comprises heat-reacting, in thepresence of a hydrogen transfer catalyst, p-phenylenediamine, with anexcess of phenol or 3,5-dimethylphenol, after introducing and sealing inthe reactor at leat 0.6 mole of hydrogen per mole of the phenol or3,5-dimethylphenol, said reaction being carried out at a temperature of130° C. to 350° C. and while converting a part of said phenol or3,5-dimethylphenol under hydrogen pressure to its correspondingcyclohexanone, and said phenol or 3,5-dimethylphenol being used in anexcess of 4 to 20 moles per mole of said p-phenylenediamine.
 4. Theprocess as claimed in claim 2 wherein the hydrogen transfer catalyst ispalladium.